Title of Invention

PROCESS FOR PRODUCTION OF A COMPOSITION USEFUL AS A FUEL

Abstract A process for the preparation of a fuel oil (diesel fuel or heating oil) composition which is a mixture of an alkanol tranesterified fatty acid ester triglyceride and an acetal of glycerol is described. The process preferably provides a prestep of the formation of at least some of the alkanol transesterif ied triglyceride containing the glycerol for use in the formation of the acetal of glycerol . The composition can also be formed from a reaction of 1,1- dimethoxy- or 1, l-diethoxye thane and glycerol to form the acetal in the alkanol transesterif ied triglyceride.
Full Text

PROCESS FOR PRODUCTION OF A COMPOSI^TION USEFUL AS A FUEL
CROSS-REFERENCE TO RELATED APPLICATIONS
[0001] This application claims priority to Provisional
Patent Application Serial No. 60/657,580, filed March 1, 2005.
STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR DEVELOPMENT
[0002] Not Applicable STATEMENT REGARDING GOVERNMENT RIGHTS [0003] Not Applicable
BACKGROUOT) OF THE INVENTION
(1) Field of the Invention
[0004] The present invention relates to a process for the
- -^■^" — preparation of a composition comprising a mixture useful as a
diesel fuel or fuel oil. In particular, the present invention
relates to a process which enables production of the
composition without the need for an intermediate separation
(extraction) step to remove a glycerol by-product ftom
transesterification of a triglyceride, such as vegetable oil,
(2) Description of the Related Art
[0005] Biodiesel is rapidly gaining momentum as the next major biofuel for-Energy sustainability. Biodiesel production in Europe is already on the order of one billion gallons annually, but U.,S. production is only 100 million gallons per year. However^- the recent spike in petroleum prices, the

increasing environmental awareness of U,S. consuraers, and the October, 2004 passage of the biodiesel tax incentive (H.R. 4 520) by Congress, providing a $1,00 per gallon tax credit for
biodiesel technologies in the U.S.
[0006] Nearly all biodiesel production from vegetable oil (triglyceride) foUov/s a common set of reaction pathways: first, tranesterification of the triglyceride with excess methanol and JJaOH catalyst to give fatty acid ester, which is the biodiesel product; then separation of the ester (^residual oil) liquid phase from the byproduct glycerol (+NaOH) phases-distillation to separate the ester from residual oil; and recovery of pure glycerol as a byproduct. The resulting methyl ester is marketed as an additive to fuel in the U.S., usually about 2% to 20% by volume, and so that the resulting composition is called 'biodiesel". There are oxygenates that can be added to the diesel fuel to promote cleaner burning as well. The uncertainty of a market for large quantities of glycerol from biodiesel and the need for continuous biodiesel production processes are two recognized challenges for large-scale biodiesel implementation-
[0007] U.S. Patent No. 6,890,364 B2 and US2004/0025417 Al to Delfort et al describe a process for producing glycerol acetals- for use in diesel fuels, and they are incorporated herein by reference in their entireties. U.S. published application 2003/0167681 Al, which is also incorporated by reference in its entirety, describes a similar two step process. The process conditions enable the formation of the acetals, with filtration of the solid and catalyst from the

composition produced, which is a mixture of acetals. The acetal mixture is added in an amount between 1 to 40%, preferably 1 to 20% by volume to diesel fuel and is soluble in the heating or diesel fuel oils which is impoprtant for preventing separation on storage. The acetal additive reduces particulate emissions, particularly from diesel engines and functions like an oxygenate.
[0008] U.S. Patent No. 5,917,059 to Bruchmann relates to a process for forming acetals. Also U.S. Patent No. 6,713,640 and 6,548,681 to Miller et al relate to a process for preparing acetals. Both references are incorporated herein by reference in their entireties.
[0009] There is a need for a more direct process for the forrp.ation of znch glycerol acetals in fuel oil compositions.
OBJECTS
[0010] It is therefore an object of the present invention to provide a process for the preparation of an oil (diesel or heating) which bypasses the need for a separation step, usually a distillation step, after the transesterification formation of the alkanol ester of the triglyceride, to remove glycerol- it is further an object of the present invention to provide a process which reliably and economically produces biologically derived fatty acid esters for use in fuel oils, such as heating
SUMMARY OF THE INVENTION
[0011] The present invention relates to a process for the preparation of a composition useful as a fuel oil which

glycerol and a lower alkanol transesterified fatty acid ester, wherein the alkanol contains 1 to 6 carbon atoms, with an aldehyde, ketone or diether containing 1 to 20 carbon atoms, acetal as a glycerol forming agent in the presence of a solid acid catalyst in a closed vessel at an elevated temperature to form a mixture of the fatty acid ester and the acetal of the glycerol to provide the composition.
[0012] The present invention relates to a process for the preparation of a composition useful as a fuel oil which
reacting in a closed vessel a mixture resulting from partial transesterification of a triglyceride with a lower alkanol containing 1 to 6 carbon atoms, the mixture comprising glycerol, monoglycerides, diglycerides, triglycerides, lower alkanol transesterified fatty acid esters, and excess alkanol, with an aldehyde^ ketone or diether containing 1 to 20 carbon atoms as a glycerol acetal forming agent in the presence of a solid acid catalyst in a closed vessel at an elevated temperature to form a mixture of the fatty acid ester and the acetal of the glycerol to provide the composition. Preferably the acetal forming agent is acetaldehyde. Preferably the lower alkanol transesterified fatty acid ester is a methyl or ethyl ester derived from a methanol or ethanol transesterification of a vegetable oil triglyceride- Preferably the aldehyde is acetaldehyde. Preferably the process is continuous. Preferably

the process comprises a preetep of partial transesterification of a triglyceride- with the alkanol to provide the mixture. Preferably the process with the prestep is continuous.

Preferably the process comprises the step of adding the alkanol to the mixture to react with unreacted triglycerides present in the mixture. Preferably the process is performed as a continuous reactive distillation with removal of the composition as it is formed. Preferably the mixture with fatty acid ester further comprises impurity amounts of free fatty acids and water.
[0013] ■ The present invention also relates to a process for the preparation of a composition useful as a fuel oil which r^omprises rf^-acting a mixture comprising 1, l-dimethoxyethane or 1,1-diethoxyethane with glycerol in a lower alcohol transesterified fatty acid ester or in the mixture described above, wherein the alkanol contains 1 to 6 carbon atoms, in the presence of a solid acid catalyst in a closed vessel, at an elevated temperature to form a mixture of the fatty acid ester and an acetal of the glycerol to provide the composition. Preferably the process comprises a further prestep,of reacting a mixture of acetaldehyde and methanol or ethanol to form the 1,1-dimethoxyethane or 1,1-diethoxyethane and then removing water formed in the reaction from the mixture. Preferably methanol or ethanol are separated from the mixture. Preferably the reaction is conducted at a pressure between about 1 at^mosphere and 27.2 atmosphere (400 psig) and at a temperature Jpetween about 80° and 200°C. r00141 The pirese.ht invention also relates to a process for

the preparation of a composition useful as a fuel froni a transesterif ied fatty acj d ester, the impx-'ovement which comprises:

a 1,1-di-methOxyethane or 1,1-diethoxyethane and water in a reaction mixture; (b) separating water from the reaction mixture; and reacting the reaction mixture of step (b) with glycerol in the rransescerified fatty acid ester from the transesterification to form a mixture of 2-methyl-4-hydroxymethyl 1,3-dioxolane and 5-hydroxymethyl-2-methyl-ly3-dioxane in the transesterified fatty acid ester as the composition. Preferably the mole ratio of methanol or ethanol to acetaldehyde in step (a) is between about 1 to 1 and 4 to 1.
• [0015] It is well known that methanol is the alcohol most used currently, to make biodiesel via a base-catalyzed, batch process. This is because methanol is inexpensive; however, methanol is advantageous from a batch processing standpoint in that it does not dissolve biodiesel or glycerol well, and thus two liquid phases are formed as reaction progresses. The batch process takes advantage of these two phases in that they offer an economical means of separating biodiesel from byproduct glycerol at the end of reaction. In the present continuous process, which involves a fixed-bed reactor and a reactive distillation column, it is desirable to maintain a single reaction phase such that all reactants can achieve intimate contact with each other. Ethanol is a substantially better

solvent than methanol for glycerol and biodiesel, such that in a relatively small e::K.ce^t5 of ethanol only a single reaction phase is present- This single phase leads to much more
is a preferred alcohol from a processing standpoint. [0016] In addition to achieving better solubilities, ethanol is a desirable component to include in biodiesel. The fatty acid ethyl esters (FAEE) that constitute *^ethyl" biodiesel have better fuel properties than fatty acid methyl esters of traditional biodiesel. Ethanol is a "green" fuel, as it is derived from renewable feedstocks such as corn and biomass. Ethanol may have better long-term price stability than methanol, which is desired from natural gas, because ethanol production processes from corn and biomass are stiill iittproving whereas natural gas prices are expected to trend even higher in the next several years. Finally, ethanol is less toxic than methanol, and diesel fuel can withstand the presence of low

[0OX7J A schematic of acetal synthesis v;ithout producing water in the transeatification reaction is as follows-.

The Bix-mertibered ring compound 5-hydroxymethyl-2-methyl-l, 3-dioxane is Tnade in nearly equal quantities to the 2-methyl-4-hydroxyraethyl-l^B-dioxolane shown above.
[0018] Acetal synthesis -without producing water in reactive distillation is important in that water liberated in glycerol acetal formation could hydrolyze methyl eBters and degrade solid acid catalysts. This can be avoided via the formation of intermediate 1,1-DME as acetal-producing species in a separate reaction vessel as a prestep. 1,1-DME (a 1,1-DEE) is then fed into the RD column, where it reacts with glycerol and liberates metha:^ol (or ethanol) .
BRIEF DESCRIPTION OF DRAWINGS
[0019] F.igure 1 is a schematic flow diagram of a process
•p^-K. i-Ho nr^Waration of the composition of the present

invention which is preferably a mixture of glycerol acetals, of acetaldehyde ' and a pre-reactor produced ethanol transestex'ified triglyceride.
scale computer modeled mass balance results from the process of Figure 1 based upon established parameters of Dhale et al, Chem. Engineering Science 2881-2890 (2004)).
[0021] ■ Figure 3 is a schematic flow diagram showing a separate acetaldehyde and alcohol reaction vessel pre-step to form 1,1-dimethylethane or 1,1-diethylethane, which is reacted with the glycerol in a main reaction vessel. (Figure 3 shows continuous biodieeel and glycerol acetal formation via 1,1-diethoxyethane (1,1-DSE> as acetalizing agent.) [0022] Picj-ure 4 is a schematic f lo^v di'^gr^iriy as a modification of Figure 1, with a.reactor vessel for oxidizing alcohol to the acetal. The partial oxidation of the alcohol to the aldehyde is an industrially practiced route to the aldehyde (acetaldehyde) formation.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
[0023] The process for biodiesel production uses reactive distillation to completely convert vegetable oil to biodiesel or fuel and while simultaneously converting glycerol to an acetal derivative suitable for inclusion in biodiesel as a fuel additive. Formation and inclusion of this acetal glycerol derivative into biodiesel is important for several reasons: 1) it adds to the overall mass yield of fuel produced; 2) it removes glycerol as it is formed during transesterification. allowina that ecfuilibrium-limited

reaction to proceed to completion; and 3) it removes the necessity and liability of downstream recovery, purification and sale, or disposal of glycerol. Moreover, the proposed Qrocess vises solid acid catalvsts such ^s ion ^rxchange r.^sin3 instead of soluble base, thus avoiding the cost of recovering and disposing of a base from the process.
[0024] The glycerol is preferably converted to its acetal derivative in situ after transesterification. The resulting glycerol acetal is thus a biodiesel fuel additive. Aldehydes or ketones readily react with vicinal diols in the presence of acid to form cyclic acetals; Scheme 1 shows the reaction of glycerol with acetaldehyde to form 4-hydroxyTOethyl-2-Tnethyl-1,3-dioxolane (HMD) and byproduct water.

Scheme 1, Formation of glycerol acetal (HMD) from glycerol and acetaldehyde,
[0025] Reaction of acetaldehyde with glycerol also forms the six-member cyclic acetal (5-hydroxytnethyl-2-methyl-1,3-dioxane) via the CI and C3 glycerol hydroxyl groups, so the final HMD product is a mixture of isomers. The acetal products are volatile (b.p. 1S0-200'*C) compounds with good combustion properties- Any aldehyde or ketone can be used, but acetaldehyde is a preferred reactant because it can be readily and reproducibly made by catalytic oxidation of ethanol. Delfort et al (cit-_^r5 7^r*^^HrMioi^T\ H=»= ^^r.^^^^-i..

reported that addition of 5 wt% glycerol acetal mixtures (HMD) to diesel fuel improves diesel fuel performance, with particulate emissions lowered by 10-30%. Thus, HMD is a good fuel additive for inclusion in the final biodi^sel product -[0026] The process is shown in Figure 1, Vegetable oil is first partially converted via transesterification in a continuous prereactor (fixed bed, stirred, bubble or other multiphase configuration) containing a solid acid catalyst. Either ethanol or methanol, or a mixture of the two, can be effectively used as the alcohol feed; methanol is cheaper, but ethanol better solubilises all species into a single phase. [0027] Because transesterification is an equilibrium-limited reaction, the prereactor column i effluent stream is a mixture of biodiesel, unreacted oil, glycerol, and alcohol. This stream is fed to the top of a continuous, countercurrent flow reactive distillation colunm 2, A mixture of alcohol and acetaldehyde are fed near the bottom of the column. Reactive distillation columns usually contain three sections or zones, an enriching zone to purify the top product, a reactive zone containing the solid catalyst in which reactions take place, and a stripping sone to purify the bottoms product. With the reactive zone of the column operating near 80°C to 200°C preferably 130'C to leCC, the volatile alcohol, aldehyde, and any water present move upward in the column as vapors, while the estisr, oil, and glycerol move downward as liquids. In the reactive zone, the alcohol contacts unreacted or partially reacted triglycerides such that further transesterification to fatty acid ester takes place. Simultaneously, acetaldehyde reacts with glycerol to form the acetal derivatives, with

product water entering Che vapor phase and exiting the top of the column away from the biodiesel product. Thus, a.s the liquid phase moves downward in the column, glycerol is converted to HMD and removed as a -oroduct. of transesterification, allowing the equilibrium biodiesel formation reaction to proceed to completion.
[0028] Pure biodiesel and HMD exit the bottom of the column with no further purification necessary. Water, alcohol, and acetaldehyde exit the top of the column, where unreacted acetaldehyde and alcohol are recovered and recycled via simple distillation.
[0029] Figure 2 shows the result of a process simulation using AspenPlus process simulation software. The simulation has been conducted by accounting for only the equilibrium phase and reaction behavior among the species in the system-It thus tests the thermodynamic feasibility of the proposed process. Two reactors ax^e simiilated - a prereactor where the feed to the process is partially converted to biodiesel, and second the reactive distillation column wherein the completion of transesterification takes place and formation of the glycerol acetals take place.
[0030] Stream 1 {triglyceride - in this case triolein, a model triglyceride) and Stream 2 (methanol) are mixed in the stirred prereactor to give 96% conversion of triglycerides and an exit Stream 3 containing small quantities of unreacted triglycerides. Stream 3 is fed to the reactive distillation column along with Stream 4, a combination of methanol and acetaldehyde. In the 15 stage column, complete conversion of triglycerides is achieved along with almost complete

conversion of glycerol to the desired glycerol acetal compounds.
[0031] The results depicted in Figure 2 indicate that the thermodynaTf.ics of the continuous biodiesel process are favorable and thus that the process is feasible from a thermodynamic viewpoint. The numbers next to the distillation column in Figure 2 are the stage numbers for feeding and withdrawing streams from the column - it can be readily observed that only a small column (15 stages) is required to complete biodiesel formation.
Economic aspects of the proposed process
[0032] Formation of HMD and its inclusion in biodiesel incurs additional cost to supply acetaldehyde, to recycle acetaldehyde and ethanol, and to remove water. These costs are offset by the alleviation of glycerol and catalyst recovery costs, by the raw catalyst cost, and by the expanded biodiesel yield realized by HMD formation. Acecaldehyde can be purchased on the spot market (the worst-case scenario) at SO.455/lb; approximately 0,5 lb acetaldehyde (MW=44) is required per lb glycerol (MW=92). Since byproduct glycerol is formed at 0.7 lb/gallon biodiesel, the acetaldehyde cost per gallon of biodiesel is $0.16 at stoichiometric consumption rates. With the molecular weight of fatty acid esters approximately 300, addition of HMD (MW=120) to biodiesel expands the yield by about 13%, or with biodiesel at $1.50 per gallon," HMD will add about $0.20/gallon in value. Thus, this shows that the cost of HMD formation is essentially offset by the additional value it brings in enhanced biodiesel yield.

Thi3 does not include the savings realized by removing glycerol froin the fuel oil and catalyst recovery from the process.
[00 3 "51 Th-s bread invention is to form the acetyl of glycerol, either the five-member or six-member ring, in a mixture with the alcohol transesterified fatty acid esters and then burn it along with the biodiesel. The acetal formation reaction nominally uses acetaldehyde to react with glycerol; indeed, chat is a straightforward reaction that proceeds to near completion. The reaction of glycerol with acetaldehyde to form the cyclic acetal liberates watery and this water could be a problem in the biodiesel formation reactions in that hydrolysis of the fatty acid methyl esters that constitute biodiesel might take place to liberate the free fatty acids, which is undesirable. As discussed previously, as an alternative, acetaldehyde are reacted with methanol to form 1,1'dimethoxyethane (CH3-CH- (OCH3)2) . The reaction involves one mole of acetaldehyde and two moles of methanol to give the 1,1-dimechoxyethane and water. The water is separated easily from the product, as 1,l-dimethoxyechane boils at 64 ""C, Dimethoxyethane is also commercially available. The same reaction can be conducted with 2 moles of ethanol and l mole of acetaldehyde to form l, 1-diethoxyethane. [0034] 1,1-dimethoxyethane or 1,1-diethoxyethane is then reacted" with glycerol to form the cyclic acetal and two moles of methanol in the reactive distillation setup. No water is formed as it is when acetaldehyde is used, so that the possible problem of biodiesel hydrolysis in the reactive distillation column because of the presence of water is

aiieviaced. Also, 1,1-diethoxyethane can be used as well. It is made from acetaldehyde and two moles of ethanol-[0035] Figure 3 shows the process with the vessels for conductinq the T»=3ctions, T-l-DEE is formed ^^^ia r??^-ct"'.on of acetaldehyde with excess ethanol over an acid catalyst in 1,1* DEE reactor, where nearly complete conversion of acetaldehyde can be obtained. If complete acetaldehyde conversion is not achieved, unreacted acetaldehyde can readily be recovered from the exit stream of the 1,1-DEE reactor by distillation, because of its low boiling point {21*'C) and recycled back to the reactor feed. Water as a reaction product is removed from the 1,1-DEB reactor exit stream by methods standard to the industry such as pressure swing adsorption using 3A molecular sieves. 1,1-DEE and ethanol are then fed to che reactive distillation column where l,l-DEE reacts with glycerol to form the glycerol acetals and ethanol. In this mode of operation, water is excluded from the reactive distillation column and thus possible hydrolysis of fatty acid esters (biodiesel) is avoided- Further, this mode of operation allows water-sensitive acid catalysts to be used in the reactive distillation column. With such water-sensitive catalysts, it is a required, standard practice to dry the triglyceride feedstock and feed ethanol prior to feeding them to the process-
[0036] In Figure 4 a pra-reactor is used to form the acetaldehyde by a conventional reaction as discussed previously. The distillate stream from the reactive distillation column contains water, alcohol, and excess, unreactP'^ ar-i&^-ftldphvde. This stream can be recovered and the

components recycled back to the stream to give the most efficient operation of the process. Acetaldehyde is removed first by regular distillation or flash, and then ethanol and water are separated either using a dedicated ethnol-water separation system involving pressure swing adsorption with molecular sievers or by returning the mixture to the ethanol-water separator in an integrated ethanol production facility. The recycle of unused reactants in the process applies to all alternate concepts in the described invention. For example, when 1,1-DEE is used as the acetal forming agent as in Figure 3, there are two components exiting the cop of the distillation column, ethanol and 1,1-DEE. These two components can foe separated by regular distillation and the individual components recycled to the process.
[0037] It is intended that the foregoing description be only illustrative of the present invention and that the present invention be limited only by the hereinafter appended claims,















WE CLAIM;
1. A process for the preparation of a composition useful as a fuel oil which comprises;
reacting in a closed vessel a mixture resulting from partial transesterif ication of a triglyceride with a lower alkanol containing 1 to $ carbon atoms, the mixture comprising glycerol, monoglycerides, diglycerides, triglycerides, lower alkanol transesterified fatty acid ester, and excess alkanol, with an aldehyde, ketone or diether containing 1 to 20 carbon atoms as a glycerol acetal forming agent in the presence of a solid acid catalyst in a closed vessel at an elevated temperature to form a mixture of the fatty acid ester and the acecal of the glycerol to provide the composition,
2. The process of Claim 1 wherein the acetal forming agent is acetaldehyde.
3 - The process of Claim 1 wherein the lower alkanol transesterified fatty acid ester is a methyl ester derived from a methanol transesterif ication of a vegetable oil triglyceride.
4. The process of Claim 1 wherein the aldehyde is acetaldehyde and the fatty acid ester is a methyl or ethyl ester derived from a methanol or ethanol transesterification of vegetable oil triglyceride.
5. The process of any one of Claims 1, 2, 3 or 4 wherein the process is continuous.

b - The process of any one of Claims 1, 2, 3, or 4 further comprising a prestep of transesterification of a triglyceride with the alkanol to provide the mixture.
7. The process of Claim 6 wherein the process with the
prestep is continuous,
8. The process of any one of Claims 1, 2, 3 or 4
wherein the acid catalyst is a resin acid catalyst.
9. The process of any one of Claims 1, 2, 3 or 4 wherein the resin acid catalyst is an acidic resin or metal oxide.
10. The process of any one of Claims 1, 2, 3, or 4 or 10 further comprising the step of adding the alkanol to the mixture to react with unreacted triglycerides present in the
mixture.
11. The process of any one of Claims 1, 2, 3, or 4, 5, 6 or 7, wherein the process is performed as a continuous reactive distillation with removal of the composition as it is formed.
12. The process of Claim 1 wherein the mixture with fatty acid ester further comprises impurity amounts of free fatty acids and water.

13- A process for the preparation of a composition useful as a fuel oil which comprises reacting a mixture comprising i, l-dimethoxyethane or 1,1-diethoxyethane with glycerol in a lower alcohol transesterified fatty acid ester, wherein the alkanol contains 1 to 6 carbon atoms, in the presence of a solid acid catalyst in a closed vessel, at an elevated temperature to form a mixture of the fatty acid ester and an acetal of the glycerol to provide the composition.
14. The process of Claim 13 further comprising a further prestep of reacting a mixture acetaldehyde and an ethyl- or methyl alcohol to form the 1, l-dimethoxyethane or 1,1-diethoxyethane and then removing water formed in the reaction from the mixture.
15. The process of Claims 13 or 14 wherein methanol or ethanol are separated from the mixture.
16. The process of Claims 14 or 15, wherein the reaction is conducted at a pressure between about 1 atmosphere and 27.2 atmosphere (4 00 psig) and at a temperature between about 80 and 200^C-
17. In a process for the preparation of a composition useful as a fuel from a transesterified fatty acid ester, the improvement which comprises:
(c) reacting methanol or ethanol with acetaldehyde to form a 1,1-di-methoxyethane or l,l-diethoxyethane and water

m a reaction mixture;
(d) separating-water from the reaction mixture; and
(e) reacting the reaction mixture of step (b) with
glycerol in the transesterifled fatty acid ester from
the .transesterification to form 2-methyl-4 -
hydroxymethyl 1,3-dioxolane in the transesterified
fatty acid ester as the composition.
18. The process of Claim 17 wherein the mole ratio of
methanol or ethanol to acetaldehyde in step (a) is
between about 1 to 1 and 4 to l.
19, A process for the preparation of a composition
useful as a fuel oil which comprises:
reacting in a closed vessel a mixture comprising glycerol and a lower alkanol transesterified fatty acid ester, wherein the alkanol contains 1 to 6 carbon atoms, with an aldehyde, ketone or diether containing 1 to 2 0 carbon atoms, acetal as a glycerol forming agent in the presence of a solid acid catalyst in a closed vessel at an elevated tempex^ature to form a mixture of the fatty acid ester and the acetal of the glycerol to provide the composition.
20. The process of Claim 19 wherein the acetal forming agent is acetaldehyde.


Documents:

3804-chenp-2007 correspondence others 28-06-2011.pdf

3804-chenp-2007 form-3 28-06-2011.pdf

3804-chenp-2007 amended pages of specification 27-06-2011.pdf

3804-chenp-2007 amended claims 27-06-2011.pdf

3804-CHENP-2007 CORRESPONDENCE OTHERS 27-06-2011.pdf

3804-chenp-2007 form-3 27-06-2011.pdf

3804-CHENP-2007 OTHER PATENT DOCUMENT 28-06-2011.pdf

3804-CHENP-2007 AMENDED PAGES OF SPECIFICATION 03-02-2011.pdf

3804-CHENP-2007 AMENDED PAGES OF SPECIFICATION 05-02-2013.pdf

3804-CHENP-2007 AMENDED CLAIMS 03-02-2011.pdf

3804-CHENP-2007 AMENDED CLAIMS 05-02-2013.pdf

3804-chenp-2007 correspondence others 09-02-2011.pdf

3804-CHENP-2007 CORRESPONDENCE OTHERS 18-12-2012.pdf

3804-CHENP-2007 CORRESPONDENCE OTHERS 31-12-2012.pdf

3804-CHENP-2007 EXAMINATION REPORT REPLY RECEIVED 03-02-2011.pdf

3804-chenp-2007 power of attorney 09-02-2011.pdf

3804-CHENP-2007 CORRESPONDENCE OTHERS 09-08-2010.pdf

3804-CHENP-2007 CORRESPONDENCE OTHERS 05-02-2013.pdf

3804-chenp-2007 form-3 03-02-2011.pdf

3804-chenp-2007-abstract.pdf

3804-chenp-2007-claims.pdf

3804-chenp-2007-correspondnece-others.pdf

3804-chenp-2007-description(complete).pdf

3804-chenp-2007-drawings.pdf

3804-chenp-2007-form 1.pdf

3804-chenp-2007-form 18.pdf

3804-chenp-2007-form 3.pdf

3804-chenp-2007-form 5.pdf

3804-chenp-2007-pct.pdf


Patent Number 258051
Indian Patent Application Number 3804/CHENP/2007
PG Journal Number 48/2013
Publication Date 29-Nov-2013
Grant Date 28-Nov-2013
Date of Filing 31-Aug-2007
Name of Patentee MICHIGAN STATE UNIVERSITY
Applicant Address 238 ADMINISTRATION BUILDING EAST LANSING MICHIGAN 48824
Inventors:
# Inventor's Name Inventor's Address
1 MILLER, DENNIS, J 5214 WHITETAIL CIRCLE OKEMOS MI 48864
2 PEEREBOOM, LARS 5981 SHOEMAN ROAD HASLETT MICHIGAN 48840
3 KOLAH, ASPI 802 CHERRY LANE APT 108 EAST LANSING MICHIGAN 48823
4 ASTHANA, NAVINCHANDRA 702 CHERRY LANE APT #105 EAST LANSING MI 48823
5 LIRA, CARL, T 131 OAKLAND DRIVE EAST LANSING MI 48823
PCT International Classification Number C10L 1/18
PCT International Application Number PCT/US06/06909
PCT International Filing date 2006-02-28
PCT Conventions:
# PCT Application Number Date of Convention Priority Country
1 60/657,580 2005-03-01 U.S.A.